Mixing method and apparatus

ABSTRACT

Method of mixing particulate materials comprising contacting a primary source and a secondary source thereof whereby resulting mixture ensues; preferably at least one of the two sources has enough motion to insure good mixing and the particulate materials may be heat treated if desired. 
     Apparatus for such mixing comprising an inlet for a primary source, a reactor communicating therewith, a feeding means for supplying a secondary source to the reactor, and an inlet for the secondary source. Feeding means is preferably adapted to supply fluidized materials.

This application is a continuation-in-part of application Ser. No.944,345 filed Sept. 21, 1978, which in turn is a continuation ofapplication Ser. No. 633,898 filed Nov. 20, 1975, now U.S. Pat. No.4,163,693, which in turn is a continuation of Ser. No. 449,073 filedMar. 7, 1974, now abandoned.

The present invention relates to a new and novel method and apparatusfor mixing particulate materials. More particularly, the inventionrelates to such a method and apparatus for the mixing of fluid mediacontaining particulate materials dispersed therein. Still moreparticularly, the invention relates to such a method and apparatus inwhich certain chemical and/or physical reactions result from suchmixing, and in which certain useful products result. Even moreparticularly, the invention relates to such a method and apparatus whichis continuous.

Coaxial fluid jet streams have been used in the past to promote theturbulent mixing thereof for the purpose of producing a well integratedcombustible mixture. Combustible mixtures have also resulted from theintroduction of a primary jet stream of a particle laden material into asecondary air stream. Such stream mixing has not been applied to mixingstreams, each containing fine particulate material, nor has it been usedas a method to transfer thermal energy between the streams.

Multiple nozzle systems for contacting multiple jet streams in order topromote the mixing thereof usually result in a high degree of abrasionin the apparatus employed because high velocities are required as arule; such systems are also characterized by a high pressure drop in theapparatus which causes lesser efficiency in the operation thereof.

Prior methods of mixing particulate materials have not been as rapid oras thorough as might be the case.

Literature relating to prior art mixing applications is found:

1. Perry, R. H., et al., Chemical Engineers Handbook, McGaw Hill (1963),pp. 5-18.

2. Hill, B. J., J. Fluid Mech., 51(4) pp. 773-779 (1972).

3. Tufts, L. W., and Smoot, L. D., J. Spacecraft, 8(12) pp. 1183-1190(1971).

It is therefore an object of the present invention to provide a new andnovel apparatus and method of mixing particulate materials.

Another object of the present invention is to provide apparatus andmethod of such types which involve contacting a source of particulatematerials of a selected type with a second source of particulatematerials of another selected type. By another selected type ofparticulate material is meant that the second solid particulate materialis different in substance from the first particulate material.

Still another object of the present invention is to provide apparatusand method of such types in which certain of the particulate materialsare first preheated before use, whereby thermal energy is transferred tothe other particulate materials in the method, upon contact.

Yet another object of the present invention is to provide apparatus andmethod for mixing particulate materials which appreciably reduce thedegree of abrasion in apparatus encountered normally in the prior art.

A further object of the present invention is to provide apparatus andmethod of the aforementioned types which significantly reduce the amountof pressure drop normally encountered in the prior art.

Still a further object of the present invention is to provide apparatusand method of the aforementioned types which are more efficient thanthose of the prior art.

Yet a further object of the present invention is to provide apparatusand method of the aforementioned types which are faster and morethorough than those of the prior art.

Other objects and advantages of the present invention will becomeapparent from a consideration of the following detailed portion of thespecification taken in conjunction with the appended drawing, in which:

FIG. 1 is an elevational view, partly in section, of apparatusincorporating one embodiment of the present invention; and

FIG. 2 is a view like FIG. 1 but incorporating another embodiment of thepresent invention; and

FIG. 3 is a view like FIG. 2 but incorporating still another embodimentof the present invention; and

FIG. 4 is a view like FIG. 3 but incorporating yet another embodiment ofthe present invention.

The present inventive method of mixing essentially involves the step ofcontacting a primary source of particulate materials and a secondarysource of particulate materials, whereby a resulting mixture ensues.Preferably the materials are then allowed to stay in contactsufficiently long enough for a desired chemical and/or physical reactionto proceed appreciably. Then preferably, desired reaction products areremoved from the resulting mixture of particulate materials.

The secondary source may be non-moving or moving, preferably relativelystagnant or slow-moving with respect to the primary source whichpreferably has more motion. The only requirement is that when the twosources are brought together, there be sufficient total motion from bothsources to insure good enough mixing of the particulate materials to beable to detect an appreciable degree of the desired chemical and/orphysical change. Preferably, the primary source is given considerablemotion and most of the mixing done thereby, while the secondary sourcegets little.

The secondary source of particulate materials may be any conventionalone, but preferably is an inert fluid medium in which the particulatematerials are dispersed; more preferably the materials are uniformlydispersed in the medium. More preferably, the fluid medium is a gaseousone and may include a mixture of gases if desired.

The particular particulate materials present in the secondary source maybe any which are desired to be brought into contact with the primarysource. In many applications, the particular particulate material ispreferably coal and/or coal chars.

The particulate materials which are preferably dispersed in a fluidmedium to form the secondary source may be dispersed by conventionalmeans, entrainment for example, but are preferably dispersed by means offluidizing the particulate materials, preferably by the gas injectionthereof or by treatment in a fluidizing chamber.

The secondary source of particulate materials preferably takes the formof a slow moving stream or entrained stream in comparison with theprimary source of particulate materials which is preferably a fastmoving stream or entraining stream. Contact of the two streams producesa resulting mixture, a stream also preferably.

The primary source of particulate materials may be conventional butpreferably is a fluid medium containing the materials, more preferably,the medium is gaseous and may include mixtures of gases if desired. Evenmore preferably, the medium is steam or an inert gas mixture. Theparticulate materials are preferably dispersed throughout the medium;more preferably, the particulate materials are preferably disperseduniformly throughout the medium.

The particular particulate materials present in the primary sourcethereof may be any having suitable properties. In many applications, thematerials are preferably the char resulting from the pyrolysis of coalor coal itself.

The particulate materials present in the primary source and preferablydispersed uniformly therein may be so dispersed by any conventionalmeans but preferably are dispersed by means of imparting turbulent flowto the source by pressurizing it sufficiently and giving it direction.Considerable motion is also imparted to the primary source as a resultwhich is useful for contacting the secondary source of particulatematerials later on.

The particulate materials of the present method may be heat treated asan additional step if desired; either the primary or the secondarysource thereof or both sources may be heat treated before or aftercontacting them together if desired. In many applications, the primarysource is preferably preheated before contact in order that the thermalenergy thereof be imparted to the secondary source of particulatematerials upon contact. More preferably, recycled char from thepyrolysis of coal is used to heat the primary source. Additionaltreatment heat may be supplied to the resulting mixture from the contactof the primary and secondary sources, if desired.

The resulting mixture, preferably a stream, from the contact of theprimary source and the secondary source contains a mixture ofparticulate materials dispersed therein which will react physicallyand/or chemically, given sufficient time. The materials in the mixtureare preferably dispersed throughout, more preferably uniformly dispersedthroughout the mixture, preferably by means of imparting a turbulentflow thereto by sufficient pressurization and by giving it direction.More preferably, the primary source is made turbulent enough initiallyto impart turbulence to the resulting mixture after contacting thesecondary source of particulate materials.

After the desired reaction has taken place, desired products areseparated from the resulting mixture. Volatile products may be taken offdirectly, resulting char may be recycled back to the present primarysource for reuse in the method, and some gas taken off and recycled backto the secondary source of particulate materials for use in fluidizingthem.

The present inventive apparatus is directed to a mixing section formixing particulate materials which has a first inlet, preferablygenerally vertically disposed, for admitting a primary source ofparticulate materials or entraining stream. The first inlet has an endwhich terminates within the mixing section which is preferablyconstricted to form a nozzle for increasing the velocity of the streamas it passes therethrough, the nozzle preferably being refractory-lined.

The mixing section also has a reactor which communicates with theaforementioned end of the first inlet to receive the entraining streamtherefrom and also communicates with a cyclone receiver which separatesgaseous and solid products from the resulting mixture after reaction hastaken place.

The mixing section further has feeding means for receiving and feedingan incoming secondary source of particulate materials or entrainedstream to the entraining stream coming in through the first inlet. Thefeeding means communicates with the reactor, providing access for asupply of particulate materials. The inlet to the reactor forms a weirmeans for the flow of the secondary source of particulate materials fromthe feeding means into the reactor. The entrained stream may enter thefeeding means from any direction or angle as long as the materialsintroduced can work their way into the reactor.

The feeding means is preferably a fluidizing means for fluidizing theincoming particulate materials. Preferably, the fluidizing means is afluidizing chamber adapted for such purposes. In some applications, thechamber is adapted to fluidize the incoming materials by impartingsufficient motion thereto. More preferably the chamber is annular andadapted to impart such motion as a result. The direction or angle atwhich the entrained stream comes into the chamber may also be adapted tohelp impart such motion thereto as may be the location of the point ofentry of the stream into the chamber and the velocity thereof.

In certain applications, the entrained stream comes into an annularchamber at a lower portion thereof and generally horizontally theretothe chamber being so adapted; more preferably, the stream comes intangentially to the chamber which is suitably adapted and a swirlingmotion is imparted as a result.

In other applications the fluidizing chamber is adapted for fluidizingby virtue of having injection means provided therewith. The injectionmeans provides apparatus for the injection of particulate materials byfluid, preferably gas, and preferably takes the form of a porous bed orplate which is adapted to operate on gas, preferably recycle gas fromthe method; the porous bed or plate allows some gas to get through itwhen pressurized sufficiently which gas does the injecting. Particulatematerials coming into the chamber are thus fluidized.

The injection means provided for the fluidizing chamber is preferablypositioned inside the chamber and more preferably at the bottom thereof.The particulate materials coming into the chamber may be introduced fromany direction or angle but are preferably introduced generallyvertically from above.

The mixing section still further has a second inlet for receiving asecondary source of particulate materials or entrained stream; thesecond inlet is connected to the feeding means, preferably generallyhorizontally at a lower portion thereof. More preferably the feedingmeans is annular and the second inlet is connected tangentially thereto.

In some applications, the second inlet is provided with additionalfluidizing means for fluidizing the particulate materials prior to entryinto the feeding chamber. The additional fluidizing means are preferablyadditional injection means and preferably an air slide connected to thesecond inlet whereby particulate materials moving through the inlet areinjected by air from the slide. More preferably, the air slide isadapted to operate on recycle gas from the method.

In other applications, the second inlet is preferably connectedsubstantially vertically to the feeding means.

Turning now to the drawing, the first three FIGS. are directed to asecondary source of particulate materials which is coal and to a primarysource of particulate materials which is char resulting from thepyrolysis of coal dispersed in stream; FIG. 4 is directed to a secondarysource of particulate material which is char resulting from thepyrolysis of coal dispersed in steam and the primary source ofparticulate materials is coal.

In FIG. 1, the char stream comes rapidly enough into the mixing section,generally designated 10, through a generally upright annular first inlet12 which has an end 14 terminating within the section and constricted at16 to form a nozzle, so that a fluid jet is formed thereby. A reactor20, also annular, has an upper end 22 which is open and of largerdiameter than the nozzle which surrounds the nozzle, leaving an openingbetween the upper end and the nozzle. In the embodiment shown in theFIGS., the inlet inside periphery of the reactor is substantially equalto the inside periphery of conduit reactor 20. In this embodiment, theinlet inside periphery is significantly greater than the outsideperiphery of the turbulent solid particulate stream forming means ornozzle 16. In general, inlet 22 of reactor 20 is completely open endedexcept for nozzle 16. In general, the opening is substantially largerthan a slit. The reactor has an elbow in the middle which rests upon asupport and has a lower end 24 connected to a cyclone receiver forseparating gaseous from solid products. An annular fluidizing chamber 28is formed by an annular section 30 which connects the first inlet andthe upper end 22 of the reactor, the chamber surrounding the nozzle anda portion of the upper end of the reactor. A second annular inlet 32 isgenerally horizontally connected to the annular fluidizing chamber at alow portion 34 thereof for receiving a stream of coal dispersed in air,the inlet also being tangentially positioned with respect to the annularchamber wall to impart a swirl to the incoming stream. Incoming coalbuilds up in the fluidizing chamber 28 and is expelled over the upperend 22 of the reactor, through the opening between the upper end thereofand the nozzle, into the reactor itself. Once inside the reactor, thecoal soon falls into the path of the turbulent fluid jet of the charstream coming from the nozzle, where it is acted upon by the jet asshown by broken lines. Once inside the reactor, the jet has a free coreregion extending considerably into the reactor but expansion of the jetalso occurs which entrains coal present, with complete mixing of thecoal and the jet later on.

In FIG. 2, the apparatus is the same as that in FIG. 1 except that thesecond annular inlet is different. The inlet 35 has a generallyhorizontal portion 36 like second inlet 32 and adapted to receive an airslide 38 and being so equipped; the air slide is preferably adapted tooperate on recycle gas instead of air. The inlet also has a generallyupright portion 40 communicating with the horizontal portion 36 throughwhich coal is introduced. Coal so vertically introduced is fluidized byinjected gas from the slide before its introduction into the fluidizingchamber.

In FIG. 3, the apparatus is the same as in FIG. 2 except that the secondannular inlet 42 for introducing coal comes generally vertically insteadof horizontally into the fluidizing chamber and in that a porous bed orplate 44 has been provided at the bottom of the chamber and connected toa source of recycle gas and adapted to operate thereon in order tofluidize such incoming coal by injecting the coal with gas.

In FIG. 4, the apparatus is similar to that of FIG. 3, except that thecoal stream is introduced through the first inlet instead of the charstream, the char stream being introduced generally vertically instead tothe fluidizing chamber from an upright second inlet 46. The flow pathsof the char and coal streams are in FIG. 4 exactly the opposite of whatthey are in FIG. 3. The coal stream in FIG. 4 is introduced rapidlyenough to form a jet stream which acts upon the char stream as shown bythe broken lines, like in FIG. 1.

In practice, a hot char recycle stream is fed to the mixing sectionshown in FIG. 1 through a seven-foot diameter vertical first inlet. Thechar stream velocity is 20 feet per second in the inlet but is increasedto 94 feet per second by passing through a nozzle 39 inches in diameterand positioned at the end of the inlet inside the mixing section.

Feed coal is pneumatically conveyed by recycle gas to the mixing sectionin a 5 inch diameter generally horizontal second inlet. The coal is thendischarged tangentially into a low portion of the annular fluidizingchamber and fluidized thereby.

The coal is then expelled over the outer wall of the reactor and throughthe open end thereof, through the opening between the open end of thereactor and the nozzle and then into the inside of the reactor where itfalls into the path of the char stream jet coming from the nozzle whichis turbulent. The reactor is annular and has the same diameter as thefirst inlet.

Fluidized coal in the reactor is entrained by the turbulent jet whichexpands once inside the reactor.

About ten feet of reactor length is required for such entrainment andanother six feet is required for the jet to disappear and the twostreams to mix completely. About 0.5 to 0.6 seconds is required forcomplete mixing.

The resulting mixture stream leaves the reactor at a velocity of 21 feetper second. The jet from the nozzle is maintained at turbulent flow byhaving a Reynolds number of 100,000. The resulting mixture stream isalso maintained at turbulent flow by having a Reynolds number of220,000.

Other details of the apparatus and method are tabulated below:

    ______________________________________                                                                   Product  Product                                           Char Recycle                                                                           Coal Feed Gas      Char                                      ______________________________________                                        Solids rate                                                                   pounds/hour                                                                             14,300,000 860,737   --     14,760,659                              Gas rate,                                                                     pounds/hour                                                                             134,794    10,000    603,502                                                                              --                                      Temperature,                                                                  Degrees                                                                       Fahrenheit                                                                              1,789      145       1,600  1,600                                   Pressure,                                                                     pounds/                                                                       sq. inch                                                                      absolute  64         66        62     62                                      Gas                                                                           Molecular                                                                     Weight    18         31.5      27     --                                      ______________________________________                                    

Some materials exhibit a plastic or tacky state when heated sufficientlywhich could plug the present mixing apparatus if used therein. Forexample, some coals exhibit this property but will lose their tackinessupon being heated sufficiently additionally; tackiness is thus atransitory state which can be overcome with sufficient heat.

Particulate materials exhibiting such tackiness can be used in thepresent apparatus without fear of plugging if they are heat treatedsufficiently, either before or during the present method. That is, ifsufficient heat is applied to the particulate materials, the tacky stateis gone through rapidly enough to avoid the problem. Preferably, theprimary or entraining stream of particulate materials is heatedsufficiently during the contacting of the secondary or entrained streamto transfer sufficient heat to get such materials in the former streamthrough the tacky state rapidly enough after mixing to avoid theplugging problem.

For example, some Eastern coals exhibit the property of tackiness whenfirst heated, but the tackiness disappears with additional heating.

Particulate material going to the reactor from the feeding means may beentrained rather than fluidized but the present apparatus and methodwould not be as efficient in operation. Such particulate material ispreferably not introduced to the reactor at very high velocity becauseit would require too high a velocity of the entraining stream otherwise.

The mixing time of the present process is dependent upon the geometry ofthe apparatus and the flow conditions of the streams. It is desirable tominimize such time.

The entraining stream or primary source of particulate materials fromthe first inlet is preferably always turbulent and is assigned anappropriate Reynolds number to insure this condition. The entrainedstream or secondary source of particulate materials from the secondinlet is preferably always maintained at a rate of flow much less thanturbulent. The resulting mixture stream from the contacting of theentraining and the entrained streams is preferably always turbulent alsoand is maintained at an appropriate Reynolds number to accomplish theresult. The relatively fast moving entraining stream thus preferablypicks up the relatively slow moving entrained stream, comparing the twostreams together, to form a resulting mixture stream which is stillfairly fast moving in comparison with the entraining stream.

The nozzle which is preferably refractory-lined may be lined with anyconventional material such as a variety of annealed stainless steel,inconel, cast steels, and the like.

In operation, an acceptable fluid velocity to the cyclone receiver isfirst selected and this velocity is chosen also for the resultingmixture stream in the reactor. Once the reactor velocity is selected,then the velocity of the entraining stream through the end, preferablyconstricted to form a nozzle, of the first inlet is picked to besubstantially higher than the reactor velocity. Then the velocity of theentrained stream is selected to provide secondary particulate materialsto the reactor at a lower velocity than the resulting mixture stream.

The velocity of the entraining stream above the nozzle does not matternor does the diameter of the first inlet as long as it is larger thanthat required for entraining the primary particulate materials. Thenozzle velocity must be substantially greater than the inlet velocityhowever.

The diameter of the nozzle does not matter as long as it issubstantially less than the inlet diameter, in order that the velocityof the entraining stream be stepped up sufficiently to operate properly.

The diameter of the reactor does not matter as long as it issignificantly greater than the nozzle diameter, so as to permit properexpansion of the jet coming into the reactor from the nozzle. The nozzlevelocity of the entraining stream entering the reactor must be greaterthan that of the resulting mixture stream, however, in order to haveflow through the reactor.

It will be apparent to those skilled in the art that all the objects andadvantages previously set forth for the present invention have beenaccomplished.

It is to be understood that only the preferred embodiments of thepresent invention have been set out and described in detail herein andthat the invention may be practiced otherwise than as specifically setforth and described and within the scope of the appended claims.

What is claimed is:
 1. A process for mixing solid particulate materialscomprising:a. introducing a first solid particulate material downwardlyand in turbulent flow into a mixing zone; b. simultaneously andseparately fluidizing a second solid particulate material in afluidizing zone with a fluidizing fluid and causing said second solidparticulate material to flow upwardly while being suspended in saidfluidizing fluid and causing said second solid particulate material tooverflow a weir means within said fluidizing zone while in the fluidizedstate and to pass from said fluidizing zone to said mixing zone, saidsecond solid particulate material being different in substance from saidfirst solid particulate material, said weir means forming an inletboundary of said mixing zone; c. introducing said second solidparticulate material into said mixing zone substantially completelyaround said first solid particulate material as said first solidparticulate material is first introduced into said mixing zone; and d.mixing said first solid particulate material and said second solidparticulate material in said mixing zone and causing by said mixing anappreciable chemical or physical change in said first or second solidparticulate material.
 2. The process of claim 1 wherein one of saidsolid particulate materials is carbonaceous and the other of said solidparticulate materials is a heated particulate.
 3. A process for mixingsolid particulate materials comprising:a. introducing a first solidparticulate material downwardly and in turbulent flow into a flowthrough mixing zone, said flow through mixing zone having an inletboundary through which said first solid particulate material isintroduced; b. simultaneously and separately fluidizing a second solidparticulate material in a fluidizing zone with a fluidizing fluid andcausing said second solid particulate material to flow upwardly whilebeing suspended in said fluidizing fluid and causing said second solidparticulate material to overflow a weir means within said fluidizingzone while in the fluidized state and to pass from said fluidizing zoneto said flow through mixing zone, said second solid particulate materialbeing different in substance from said first solid particulate material,said weir means forming said inlet boundary of said mixing zone; c.introducing said second solid particulate material into said flowthrough mixing zone through and substantially completely around and incontact with said inlet boundary of said flow through mixing zone; andd. mixing said first solid particulate material and said second solidparticulate material in said flow through mixing zone and causing bysaid mixing an appreciable chemical or physical change in said first orsecond solid particulate material.
 4. A process for mixing solidparticulate materials comprising:a. introducing a first solidparticulate material downwardly and in turbulent flow into a flowthrough conduit reactor having a substantially vertically inclined andsubstantially completely open ended inlet; b. simultaneously andcontinuously fluidizing a second solid particulate material in afluidizing chamber which surrounds said inlet of said conduit reactorand which contains a weir means formed by said inlet of said conduitreactor and said fluidizing chamber, with a fluidizing gas and causingsaid second solid particulate material to flow upwardly while beingsuspended in said fluidizing gas and causing said second solidparticulate material to overflow said weir means and to enter said inletof said reactor completely around said first solid particulate as saidfirst solid particulate enters said inlet of said reactor, said secondsolid particulate material being different in substance from said firstsolid particulate material, said weir means forming an inlet boundary ofsaid mixing zone; and c. mixing said first solid particulate materialand said second solid particulate material and causing by said mixing anappreciable chemical or physical change in said first or second solidparticulate material.
 5. A process for mixing solid particulatematerials comprising:a. introducing a first solid particulate materialdownwardly and in turbulent flow into a mixing zone; b. simultaneouslyand separately fluidizing a second solid particulate material in afluidizing zone with a fluidizing fluid and causing said second solidparticulate material to flow upwardly while being suspended in saidfluidizing fluid and causing said second solid particulate material tooverflow a weir means within said fluidizing zone while in the fluidizedstate and to pass from said fluidizing zone to said mixing zone, saidweir means forming an inlet boundary of said mixing zone; c. introducingsaid second solid particulate material into said mixing zonesubstantially completely around said first solid particulate material assaid first solid particulate material is first introduced into saidmixing zone; and d. mixing said first solid particulate material andsaid second solid particulate material in said mixing zone and causingby said mixing an appreciable chemical or physical change in said firstor second solid particulate material; wherein one of said solidparticulate material is coal and the other of said solid particulatematerials is a heated solid particulate which is different in substancefrom said coal.
 6. The process for mixing solid particulate materialscomprising:a. introducing a first solid particulate material downwardlyand in turbulent flow into a flow through mixing zone, said flow throughmixing zone having an inlet boundary through which said first solidparticulate material is introduced; b. simultaneously and separatelyfluidizing a second solid particulate material in a fluidizing zone witha fluidizing fluid and causing said second solid particulate material toflow upwardly while being suspended in said fluidizing fluid and causingsaid second solid particulate material to overflow a weir means withinsaid fluidizing zone while in the fluidized state and to pass from saidfluidizing zone to said flow through mixing zone, said weir meansforming said inlet boundary of said mixing zone; c. introducing saidsecond solid particulate material into said flow through mixing zonethrough and substantially completely around said inlet boundary of saidflow through mixing zone; and d. mixing said first solid particulatematerial and said second solid particulate material in said flow throughmixing zone and causing by said mixing an appreciable chemical orphysical change in said first or second solid particulate material;wherein one of said solid particulate materials is coal and the other ofsaid solid particulate materials is a heated solid particulate which isdifferent in substance from said coal.
 7. A process for mixing solidparticulate materials comprising:a. introducing a first solidparticulate material downwardly and in turbulent flow into a flowthrough conduit reactor having a substantially vertically inclined andsubstantially completely open ended inlet; b. simultaneously andcontinuously fluidizing a second solid particulate material in afluidizing chamber which surrounds said inlet of said conduit reactorand which contains a weir means formed by said inlet of said conduitreactor and said fluidizing chamber, with a fluidizing gas and causingsaid second solid particulate material to flow upwardly while beingsuspended in said fluidizing gas and causing said second solidparticulate material to overflow said weir means and to enter said inletof said reactor completely around said first solid particulate as saidfirst solid particulate enters said inlet of said reactor, said weirmeans forming an inlet boundary of said mixing zone; and c. mixing saidfirst solid particulate material and said second solid particulatematerial and causing by said mixing an appreciable chemical or physicalchange in said first or second solid particulate material; wherein oneof said solid particulate materials is coal and the other of said solidparticulate materials is a heated solid particulate which is differentin substance from said coal.
 8. The process of claim 7 wherein saidfirst solid particulate material is introduced into said flow throughconduit reactor substantially centrally.
 9. The process of claim 7wherein said coal is a type which exhibits a plastic or tacky state whenheated sufficiently.
 10. The process of claim 7 further comprisingremoving said solid particulate materials from said flow through conduitreactor after said mixing thereof.
 11. The process of claim 7 furthercomprising entraining said first solid particulate material in a gasstream before introducing said first solid particulate material intosaid flow through conduit reactor.
 12. A process for mixing solidparticulate materials using an apparatus comprising a conduit reactorhaving an inlet and an outlet, said inlet being substantially verticallyinclined and substantially completely open ended, said inlet having aperiphery, said inlet having an inlet inside periphery equal to theinside periphery of said conduit reactor, a turbulent solid particulatestream forming means having an inlet for introducing a first solidparticulate material thereto, and an outlet directed substantiallydownwardly into said inlet of said conduit reactor for introducing aturbulent solid particulate stream into said conduit reactor, said inletinside periphery being significantly greater than the outside peripheryof said turbulent solid particulate stream forming means, said inletbeing completely open ended except for said turbulent solid particulatestream forming means, a fluidizing means surrounding said periphery ofsaid inlet of said conduit reactor for fluidizing a second solidparticulate material around said periphery of said inlet of said conduitreactor, and a weir means formed by said inlet of said conduit reactorand said fluidizing means and extending into said fluidizing means, saidprocess comprising:a. introducing said first solid particulate materialdownwardly and in turbulent flow into said conduit reactor through saidturbulent solid particulate stream forming means; b. simultaneously andseparately fluidizing said second solid particulate material in saidfluidizing means with a fluidizing fluid and causing said second solidparticulate material to flow upwardly while being suspended in saidfluidizing fluid and causing said second solid particulate material tooverflow said weir means; c. introducing said second solid particulatematerial into said conduit reactor substantially completely around saidfirst solid particulate material as said first solid particulatematerial is first introduced into said conduit reactor; and d. mixingsaid first solid particulate material and said second solid particulatematerial in said conduit reactor and causing by said mixing anappreciable chemical or physical change in said first or second solidparticulate material; wherein one of said solid particulate materials iscoal and the other of said solid particulate materials is a heated solidparticulate which is different in substance from said coal.
 13. Theprocess of claim 12 wherein said turbulent solid particulate streamforming means extends below said periphery of said inlet of said conduitreactor.
 14. The process of claim 12 wherein said turbulent solidparticulate stream forming means comprises a nozzle.
 15. The process ofclaim 12 wherein said inlet of said conduit reactor is annular incross-section.
 16. A process for mixing solid particulate materialsusing an apparatus comprising a conduit reactor having an inlet and anoutlet, said inlet being substantially vertically inclined andsubstantially completely open ended, said inlet having an inlet insideperiphery equal to the inside periphery of said conduit reactor, aturbulent solid particulate stream forming means having an inlet forintroducing a first solid particulate material thereto, and an outletdirected substantially downwardly into said inlet of said conduitreactor for introducing a turbulent solid particulate stream into saidconduit reactor, said inlet inside periphery being significantly greaterthan the outside periphery of said turbulent solid particulate streamforming means, said inlet being completely open ended except for saidturbulent solid particulate stream forming means, a fluidizing chambercommunicating with said conduit reactor through said inlet of saidconduit reactor, said fluidizing chamber having an inlet for introducinga second solid particulate material thereto, an inlet for introducing afluidizing fluid thereto, and an outlet defined by an opening betweensaid inlet of said conduit reactor and said outlet of said turbulentsolid particulate stream forming means; and a weir means formed by saidinlet of said conduit reactor and said fluidizing chamber and extendinginto said fluidizing chamber, said process comprising:a. introducingsaid first solid particulate material downwardly and in turbulent flowinto said conduit reactor through said turbulent solid particulatestream forming means; b. simultaneously and separately fluidizing saidsecond solid particulate material in said fluidizing chamber with saidfluidizing fluid and causing said second solid particulate material toflow upwardly while being suspended in said fluidizing fluid and causingsaid second solid particulate material to overflow said weir means; c.introducing said second solid particulate material into said conduitreactor substantially completely around said first solid particulatematerial as said first solid particulate material is first introducedinto said conduit reactor; and d. mixing said first solid particulatematerial and said second solid particulate material in said conduitreactor and causing by said mixing an appreciable chemical or physicalchange in said first or second solid particulate material; wherein oneof said solid particulate materials is coal and the other of said solidparticulate materials is a heated solid particulate which is differentin substance from said coal.
 17. A process for mixing solid particulatematerials using an apparatus comprising a conduit reactor having aninlet and an outlet, said inlet being substantially vertically inclinedand substantially completely open ended, said inlet having an inletinside periphery equal to the inside periphery of said conduit reactor,a turbulent solid particulate stream forming means having an inlet forintroducing a first solid particulate material thereto, and an outletdirected substantially downwardly and substantially centrally into saidinlet of said conduit reactor for introducing a turbulent solidparticulate stream into said conduit reactor, said inlet insideperiphery being significantly greater than the outside periphery of saidturbulent solid particulate stream forming means, said inlet beingcompletely open ended except for said turbulent solid particulate streamforming means, a fluidizing chamber communicating with said conduitreactor through said inlet of said conduit reactor and surrounding saidinlet of said conduit reactor, said fluidizing chamber having an inletfor introducing a second solid particulate material thereto, an inletfor introducing a fluidizing fluid thereto, and an outlet defined by anopening between said inlet of said conduit reactor and said outlet ofsaid turbulent solid particulate stream forming means; and a weir meansformed by said inlet of said conduit reactor and said fluidizing chamberand extending into said fluidizing chamber; said process comprising:a.introducing said first solid particulate material downwardly and inturbulent flow into said conduit reactor through said turbulent solidparticulate stream forming means; b. simultaneously and separatelyfluidizing said second solid particulate material in said fluidizingchamber with said fluidizing fluid and causing said second solidparticulate material to flow upwardly while being suspended in saidfluidizing fluid and causing said second solid particulate material tooverflow said weir means while in the fluidized state; c. introducingsaid second solid particulate material into said conduit reactorsubstantially completely around said first solid particulate material assaid first solid particulate material is first introduced into saidconduit reactor; and d. mixing said first solid particulate material andsaid second solid particulate material in said conduit reactor andcausing by said mixing an appreciable chemical or physical change insaid first or second solid particulate material; wherein one of saidsolid particulate materials is coal and the other of said solidparticulate materials is a heated solid particulate which is differentin substance from said coal.
 18. The process of claim 17 wherein saidturbulent solid particulate stream forming means extends below saidinlet of said conduit, and comprises a nozzle, wherein said inlet ofsaid conduit reactor is annular in cross-section.